WO2012057176A1 - Procédé de traitement de l'eau et procédé de dessalement - Google Patents

Procédé de traitement de l'eau et procédé de dessalement Download PDF

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Publication number
WO2012057176A1
WO2012057176A1 PCT/JP2011/074617 JP2011074617W WO2012057176A1 WO 2012057176 A1 WO2012057176 A1 WO 2012057176A1 JP 2011074617 W JP2011074617 W JP 2011074617W WO 2012057176 A1 WO2012057176 A1 WO 2012057176A1
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WO
WIPO (PCT)
Prior art keywords
water
solid
liquid separation
separation unit
membrane
Prior art date
Application number
PCT/JP2011/074617
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English (en)
Japanese (ja)
Inventor
花田茂久
伊藤世人
Original Assignee
東レ株式会社
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Publication date
Application filed by 東レ株式会社 filed Critical 東レ株式会社
Priority to CN2011800499103A priority Critical patent/CN103153876A/zh
Priority to JP2012511469A priority patent/JPWO2012057176A1/ja
Publication of WO2012057176A1 publication Critical patent/WO2012057176A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
    • B01D2321/18—Use of gases
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases

Definitions

  • the present invention relates to a water treatment method for producing high-quality water such as drinking water and industrial water by membrane treatment of raw water such as seawater, river water, and sewage secondary treated water.
  • One of the methods for producing high-quality water from raw water such as seawater is a water treatment method using a reverse osmosis membrane or a nanofiltration membrane. Since the raw water contains solid components such as turbidity, when the raw water is directly subjected to membrane filtration, the solid components adhering to the membrane surface increase and the differential pressure rises rapidly. Therefore, it is necessary to pre-treat raw water in advance, and the most frequently used method is a coagulating sand filtration method in which a flocculant is added to the raw water to solidify the solid components and filter with sand or anthracite. However, since this method is easily affected by fluctuations in raw water and the quality of treated water is unstable, membrane pretreatment in which treated water is treated with a microfiltration membrane or an ultrafiltration membrane has recently been adopted.
  • Patent Document 4 describes that by adding a reducing agent such as sodium hydrogen sulfate and sodium thiosulfate intermittently, the growth of microorganisms can be suppressed and the increase in membrane differential pressure can be reduced. Yes.
  • the present invention provides a water treatment method in which filtered water obtained by solid-liquid separation of water to be treated by a solid-liquid separation unit is treated with a reverse osmosis membrane or a nanofiltration membrane, and reverse osmosis without newly adding chemicals.
  • the purpose is to suppress biofouling of membranes and nanofiltration membranes.
  • the present invention for solving this problem is specified as follows.
  • a water treatment method for treating filtered water obtained by solid-liquid separation of water to be treated having a dissolved oxygen concentration of 1 mg / L or more by a solid-liquid separation unit with a reverse osmosis membrane and / or a nanofiltration membrane A water treatment method comprising performing gas cleaning for cleaning the solid-liquid separation unit with deoxygenated gas so that the dissolved oxygen concentration in the filtrate falls to 0.5 mg / L or less.
  • a method for producing fresh water characterized by performing gas cleaning in which the solid-liquid separation unit is cleaned with deoxygenated gas so that the dissolved oxygen concentration in the filtered water is reduced to 0.5 mg / L or less.
  • the present invention by washing the solid-liquid separation unit with deoxygenated gas, not only can the solid components clogged in the solid-liquid separation unit be washed away, but also the water to be treated can be added without newly adding chemicals.
  • the water to be treated can be added without newly adding chemicals.
  • FIG. 1 It is a schematic flowchart which shows an example of the apparatus which enforces the water treatment method of this invention.
  • Example 1 When cleaning with deoxygenated gas (Example 1), when cleaning with air (Comparative Example 1), and when the amount of cleaning air of deoxygenated gas is less than that of Example 1 (Comparative Example 2) And the transition of the dissolved oxygen concentration in filtered water in the case of using both cleaning with deoxygenated gas and cleaning with air (Comparative Example 3) is shown.
  • the water treatment method of the present invention is a water treatment in which filtered water obtained by solid-liquid separation of water to be treated having a dissolved oxygen concentration of 1 mg / L or more by a solid-liquid separation unit is treated by a reverse osmosis membrane and / or a nanofiltration membrane. Implemented in the method.
  • water to be treated examples include seawater, river water, lake water, ground water, sewage secondary treated water, etc., and since the effect of carrying out the present invention appears remarkably, the dissolved oxygen concentration of the water to be treated Is preferably 1 mg / L or more.
  • the solid-liquid separation unit separates and removes solid components such as turbidity contained in the water to be treated.
  • deoxygenated gas is used to wash the solid components clogged in the solid-liquid separation unit. It has a mechanism to supply Thereby, the effect by implementing this invention is acquired.
  • Specific examples of the solid-liquid separation unit include a membrane filtration device using a microfiltration membrane and an ultrafiltration membrane, and a filtration device laid with a filter medium such as sand and anthracite.
  • the mechanism for supplying the deoxygenated gas is not particularly limited.
  • the compressed deoxygenated gas is pressure-adjusted by a regulator and then supplied to the solid-liquid separation unit.
  • the reverse osmosis membrane and nanofiltration membrane that can be used in the present invention are made of any material as long as the salt concentration can be lowered so that the water to be treated can be used for drinking water, industrial water, city water, etc. May be used, for example, those composed of cellulose acetate-based and polyamide-based materials.
  • what is particularly effective in the method of the present invention is composed of a polyamide-based material.
  • Polyamide-based membranes have low resistance to chlorine, which is most commonly used as a bactericidal agent, and even when only a small concentration of chlorine is used, membrane degradation occurs remarkably, making it difficult to prevent biofouling. Therefore, the effect by implementing this invention appears notably.
  • the solid-liquid separation unit is washed with deoxygenated gas so that the dissolved oxygen concentration in the filtrate obtained by solid-liquid separation by the solid-liquid separation unit is reduced to 0.5 mg / L or less.
  • the solid component clogged in the solid-liquid separation unit is washed and removed.
  • ⁇ ⁇ max ⁇ S O2 / (K O2 + S O2 )
  • ⁇ specific growth rate of microorganism [1 / d]
  • ⁇ max maximum specific growth rate [1 / d]
  • S O2 dissolved oxygen concentration [mg / L]
  • K O2 half-saturation constant of dissolved oxygen [Mg / L].
  • K O2 Although the value of K O2 depends on the type of microorganism, it is generally about 0.5 [mg / L]. Therefore, by reducing the dissolved oxygen concentration to 0.5 mg / L or less, the growth rate of microorganisms can be reduced to 1 ⁇ 2 or less. Based on this, in the present invention, it is preferable to lower the dissolved oxygen concentration in the filtered water solid-liquid separated by the solid-liquid separation unit to 0.5 mg / L or less. Here, it is preferable to confirm that the concentration is 0.5 mg / L or less by, for example, installing a dissolved oxygen meter equipped with a diaphragm electrode in a filtered water tank and monitoring the dissolved oxygen concentration.
  • the deoxygenated gas only needs to be able to drive out dissolved oxygen by blowing it into the solid-liquid separation unit, and examples thereof include nitrogen gas, helium gas, and argon gas.
  • the gas cleaning may be performed constantly, it is preferable to perform the cleaning intermittently in consideration of cost.
  • the time when the dissolved oxygen concentration in the filtered water is 0.5 mg / L or less is half or more of the entire operation time of the solid-liquid separation unit.
  • the “total operation time of the solid-liquid separation unit” refers to the entire time required for each step of filtration and washing, water supply, and drainage in the solid-liquid separation unit.
  • Example 1 Seawater (dissolved oxygen concentration 7 mg / L) was treated water, and treated water 1 was treated by a treatment method as shown in FIG.
  • water 1 to be treated is placed in a dipping tank 2 (effective capacity: 350 L) in which a separation membrane 3 (polyvinylidene fluoride hollow fiber ultrafiltration membrane (LSU-1515 manufactured by Toray), membrane area: 50 m 2 ) is immersed.
  • the water to be treated was filtered through the separation membrane 3. Filtration was performed with a suction pump 4 and the filtration flux was 1 m / d.
  • the filtered water 5 is passed through a cartridge filter 7 having a pore size of 5 ⁇ m (Loki Techno SLS-050) with a water pump 6, and then water is supplied to the reverse osmosis membrane device 9 with a high-pressure pump 8, and filtered. Water 10 and concentrated water 11 were obtained.
  • a reverse osmosis membrane a spiral type reverse osmosis membrane device (TM810C manufactured by Toray) having a membrane material of polyamide, a desalination rate of 99.75%, and a membrane area of 7.8 m 2 is operated in series. went. The operation was set to a membrane filtration flux of 14 L / m 2 / hr and a recovery rate of 37%. This recovery rate is calculated by the flow rate of the permeated water 10 / (flow rate of the permeated water 10 + flow rate of the concentrated water 11) ⁇ 100.
  • the operation of the separation membrane 3 was performed in a cycle shown in Table 1 in 35 minutes per cycle.
  • the water 1 to be treated was supplied to the immersion tank 2 for 2 minutes to fill the water, and then washed with nitrogen gas 12 (air volume: 100 L / min) to expel dissolved oxygen from the water to be treated.
  • nitrogen gas 12 air volume: 100 L / min
  • filtration was performed for 9 minutes.
  • a water level sensor was provided in the immersion tank, and when it reached a low water level during filtration, water was automatically supplied until the water level became full.
  • back pressure washing and nitrogen washing were simultaneously performed. Back pressure washing was performed by flowing filtered water 5 from the filtration side at a rate of 52 L / min. The nitrogen cleaning was performed at an air volume of 100 L / min.
  • the transition of dissolved oxygen concentration in the filtrate 5 during operation is shown in FIG. Since water supply is performed in the middle of the filtration step, it is not always 0.5 mg / L or less, but 0.5 mg / L or less was maintained for more than half of the entire operation time of the solid-liquid separation unit.
  • the operation differential pressure the pressure difference between the reverse osmosis membrane raw water and the concentrated water (hereinafter referred to as the operation differential pressure) was constantly monitored, but the operation differential pressure was about 30 kPa from about 30 kPa. There was only a slight increase to 33 kPa.
  • Example 1 The operation was performed in the same manner as in Example 1 except that cleaning with air was performed instead of cleaning with nitrogen gas.
  • FIG. 2 shows the transition of dissolved oxygen concentration in the filtered water 5 during operation. The dissolved oxygen concentration changed between 7 and 8 mg / L. As a result, the operation differential pressure of the reverse osmosis membrane rose from about 30 kPa to about 100 kPa after 2 months of operation, and chemical solution cleaning had to be performed.
  • Example 2 shows the transition of dissolved oxygen concentration in the filtered water 5 during operation.
  • the dissolved oxygen concentration remained at about 1 mg / L without being lowered to 0.5 mg / L or less even after nitrogen cleaning.
  • the operation differential pressure of the reverse osmosis membrane rose from about 30 kPa to about 100 kPa after 2 months of operation, and chemical solution cleaning had to be performed.
  • FIG. 2 shows the transition of dissolved oxygen concentration in the filtered water 5 during operation. Of the 35 minutes of one cycle (27 minutes of filtration time), the dissolved oxygen concentration was 0.5 mg / L or less only in the initial 6 minutes. As a result, the operation differential pressure of the reverse osmosis membrane rose from about 30 kPa to about 100 kPa after 2 months of operation, and chemical solution cleaning had to be performed.
  • the present invention provides drinking water and industrial water by subjecting raw water such as seawater, river water, and sewage secondary treated water to solid-liquid separation using a solid-liquid separation unit, and membrane treatment with a reverse osmosis membrane or a nanofiltration membrane.
  • raw water such as seawater, river water, and sewage secondary treated water
  • membrane treatment with a reverse osmosis membrane or a nanofiltration membrane For example, it can be suitably used as a method for producing high-quality water.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Nanotechnology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Physical Water Treatments (AREA)

Abstract

L'invention concerne un procédé de traitement de l'eau dans lequel de l'eau filtrée, obtenue à l'aide d'une unité de séparation solide-liquide pour effectuer une séparation solide-liquide sur de l'eau non traitée ayant un taux d'oxygène dissous de 1 mg/L ou plus, est traitée à l'aide d'une membrane d'osmose inverse et/ou d'une membrane de nanofiltration. La réalisation d'un nettoyage par gaz, suivant lequel un gaz désoxydant est utilisé pour nettoyer l'unité de séparation solide-liquide de sorte que le taux d'oxygène dissous de l'eau filtrée précédemment mentionnée tombe à 0,5 mg/L ou moins, rende minimal l'encrassement biologique de la membrane d'osmose inverse ou de la membrane de nanofiltration, sans utilisation d'additifs chimiques, lors de la fabrication d'eau de haute qualité telle que de l'eau de boisson ou de l'eau industrielle à l'aide d'une membrane d'osmose inverse ou d'une membrane de nanofiltration pour effectuer un traitement sur membrane de l'eau filtrée obtenue à l'aide d'une unité de séparation solide-liquide pour effectuer une séparation solide-liquide sur de l'eau non traitée telle que de l'eau de mer, des eaux fluviales ou des eaux usées après un traitement secondaire.
PCT/JP2011/074617 2010-10-29 2011-10-26 Procédé de traitement de l'eau et procédé de dessalement WO2012057176A1 (fr)

Priority Applications (2)

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CN2011800499103A CN103153876A (zh) 2010-10-29 2011-10-26 水处理方法和造水方法
JP2012511469A JPWO2012057176A1 (ja) 2010-10-29 2011-10-26 水処理方法および造水方法

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JP2010-243054 2010-10-29
JP2010243054 2010-10-29

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110240300A (zh) * 2019-06-26 2019-09-17 凌叙根 一种带有多层纳米滤膜的净水设备
NL2027905B1 (en) * 2021-04-01 2022-10-17 Allied Waters B V A method for producing tailored quality water.

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112646975B (zh) * 2020-12-17 2021-11-05 紫金矿业集团股份有限公司 铜矿酸性萃余液减量化和资源化的处理方法

Citations (5)

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Publication number Priority date Publication date Assignee Title
JPH0295422A (ja) * 1988-09-30 1990-04-06 Akua Runesansu Gijutsu Kenkyu Kumiai 中空糸膜モジュールの運転方法
JP2007524501A (ja) * 2003-06-24 2007-08-30 カロロ エンジニアーズ， ピー・シー 廃水処理の方法および廃水処理のシステム
JP2008183510A (ja) * 2007-01-30 2008-08-14 Toray Ind Inc 浄化水の製造方法およびその製造装置
JP2009530072A (ja) * 2006-03-16 2009-08-27 シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ 液体流から金属硫化物粒子を除去する方法及び装置
JP2010069361A (ja) * 2008-09-16 2010-04-02 Mitsubishi Rayon Eng Co Ltd 膜洗浄装置、膜分離装置および排水処理装置

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1176032C (zh) * 2002-09-24 2004-11-17 天津大学 一种电子级水的集成膜过程生产方法
CN201305523Y (zh) * 2008-11-12 2009-09-09 恩那社(上海)水处理系统有限公司 一种将中水转化为超纯水的处理系统

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH0295422A (ja) * 1988-09-30 1990-04-06 Akua Runesansu Gijutsu Kenkyu Kumiai 中空糸膜モジュールの運転方法
JP2007524501A (ja) * 2003-06-24 2007-08-30 カロロ エンジニアーズ， ピー・シー 廃水処理の方法および廃水処理のシステム
JP2009530072A (ja) * 2006-03-16 2009-08-27 シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ 液体流から金属硫化物粒子を除去する方法及び装置
JP2008183510A (ja) * 2007-01-30 2008-08-14 Toray Ind Inc 浄化水の製造方法およびその製造装置
JP2010069361A (ja) * 2008-09-16 2010-04-02 Mitsubishi Rayon Eng Co Ltd 膜洗浄装置、膜分離装置および排水処理装置

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110240300A (zh) * 2019-06-26 2019-09-17 凌叙根 一种带有多层纳米滤膜的净水设备
NL2027905B1 (en) * 2021-04-01 2022-10-17 Allied Waters B V A method for producing tailored quality water.

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CN103153876A (zh) 2013-06-12
JPWO2012057176A1 (ja) 2014-05-12

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